|Número da publicação||US4695320 A|
|Tipo de publicação||Concessão|
|Número do pedido||US 06/786,903|
|Data de publicação||22 set. 1987|
|Data de depósito||11 out. 1985|
|Data da prioridade||11 out. 1985|
|Status da taxa||Sem validade|
|Número da publicação||06786903, 786903, US 4695320 A, US 4695320A, US-A-4695320, US4695320 A, US4695320A|
|Inventores||Roy A. Christini, Kenneth P. Frizzell|
|Cessionário original||Aluminum Company Of America|
|Exportar citação||BiBTeX, EndNote, RefMan|
|Citações de patente (7), Citações de não patente (5), Citada por (5), Classificações (5), Eventos legais (5)|
|Links externos: USPTO, Cessão do USPTO, Espacenet|
The invention relates generally to a process for refining crude magnesium metal and, more particularly, to a process for increasing the recovery of magnesium from magnesium crude containing high levels of calcium.
Thermal reduction processes such as the Magnetherm Process (i.e., disclosed in U.S. Pat. No. 2,971,833) produce or recover magnesium containing high levels of calcium (hereinafter referred to as magnesium crude) since the magnesium source ore typically contains high levels of calcium. Conventional commercial processes remove calcium and alkali metals, in addition to various oxides in the crude, by mixing various flux compositions into a crucible containing a molten body of the crude. These fluxes wash the oxides from the crude and react with calcium and the alkali metals to produce a sludge containing calcium chloride, the alkali metal chlorides and oxides. The sludge, being more dense than the crude, settles to the bottom of the crucible thereby enabling the now refined crude to be separated from the sludge. The separated, refined magnesium can then be cast directly into ingots. One flux which has been commercially used to refine magnesium crude contains approximately 40 wt. % magnesium chloride, 55 wt. % potassium chloride and 5 wt. % calcium fluoride and will be referred to hereinafter as M-130 flux.
Sludge produced by the above refining operation generally contains a certain residual but significant amount of magnesium which can also be recovered if subjected to another fluxing operation which is hereinafter referred to as the reclaiming operation or reclaim step. Fluxes which are typically used to reclaim such sludges include M-130, pure potassium chloride and aluminum fluoride, and various combinations thereof.
The use of fluxes to refine or purify magnesium and various other metals and alloys is discussed in U.S. Pat. Nos. 1,524,470, 1,754,788, 4,099,965 and German Patent No. 122,312. While most of these processes presumably work as intended, there is always a need for processes that work better.
An object of the present invention is to provide a process which increases the recovery of magnesium from magnesium crude.
Another object of the present invention is to provide a process for refining magnesium crude which produces a sludge capable of being reclaimed at low temperatures.
Yet another object of the present invention is to provide a process for refining magnesium crude which uses less refining flux, thereby reducing flux costs.
The present invention provides a process for refining magnesium crude containing between about 0.7 and 1.5 wt. % calcium. The process includes mixing a flux containing from about 55 to 85 wt. % magnesium chloride and 45 to 15 wt. % alkali chlorides into a molten body of the crude. Refined magnesium is thereby produced, as well as a sludge containing calcium chloride which never has a liquidus exceeding the temperature of the molten body. The refined magnesium is then separated from the sludge.
The sole FIGURE is a ternary phase diagram illustrating liquidus temperatures for all compositions in a KCl-CaCl2 -MgCl2 system.
The flux composition for increasing the recovery of magnesium from unrefined magnesium crude in accordance with the process of the present invention can contain from about 55 to 85 wt. % magnesium chloride and 45 to 15 wt. % alkali chlorides, with potassium chloride being the preferred alkali chloride. A more preferred flux composition for use in the process of the present invention can contain from 60 to 80 wt. % magnesium chloride and 40 to 20 wt. % potassium chloride. A typical flux composition for use in the refining process of the process invention contains between about 60 and 70 wt. % magnesium chloride, 40 to 30 wt. % potassium chloride and 0 to 5 wt. % aluminum fluoride.
As previously mentioned, magnesium crude produced by thermal reduction processes, such as the Magnetherm Process, generally contains high levels of calcium, typically between about 0.7 to 1.5 wt. %. To remove this calcium from the crude, fluxes containing magnesium chloride are mixed into a molten body of crude contained in a crucible. The magnesium chloride reacts with the calcium in the crude to produce a sludge containing calcium chloride which settles to the bottom of the crucible. Since the sludge's composition continually changes as the reaction proceeds (i.e., as MgCl2 is replaced by CaCl2), the sludge can freeze or at least become semi-molten since different sludge compositions can have drastically different liquidus temperatures, some of which may approach the temperature of the molten body of crude which is generally held close to about 730° C. (See sole FIGURE which is a ternary phase diagram illustrating the liquidus temperature of all compositions in a KCl-CaCl2 -MgCl2 system.) Frozen or even semi-molten sludge is desirably avoided since it tends to entrap magnesium in the sludge, thereby reducing recoveries. Moreover, the reclaim of frozen or semi-molten sludges is very difficult. Accordingly, to prevent the sludge from freezing or becoming semi-molten, a flux should be selected that will produce a sludge having a composition that never changes to the point where its liquidus exceeds the crude's temperature. Preferably, the sludge's liquidus should be well below the crude's temperature, preferably at least 70 centigrade degrees below.
The liquidus of the sludge generated when using conventional M-130 flux generally stays below the crude's temperature. The line going from point A to point B in the sole FIGURE illustrates the various liquiduses of the various sludge compositions which are produced as the reaction proceeds with conventional M-130. Point A approximates M-130's composition at the start of the reaction which, as can be seen on the diagram, is approximately 45% magnesium chloride, 55% potassium chloride. It can also be seen that this flux has a liquidus of only 440° C., which is well below that of magnesium. Point B represents the theoretical composition of the sludge after complete reaction of the magnesium chloride with the calcium contained in the crude. In reality, however, the reaction with M-130 flux only proceeds to about point C (i.e., liquidus of 680° C.) and the sludge at this point usually contains approximately 6 to 9 wt. % magnesium chloride. It can also be seen on the diagram that the liquidus of the sludge gradually increases as its composition changes from point A to point C. While the liquidus of M-130 produced sludge never exceeds the crude's temperature, at 680° C. it comes quite close which makes the sludge reclaim step somewhat difficult. Thus, it would be desirable if the final sludge had a lower liquidus, even slightly lower, since this would enable the reclaim operation to be carried out at lower temperatures.
Line XY illustrated in the sole FIGURE illustrates liquidus and compositional changes for a sludge which is generated by a flux composition of the present invention. Point X represents the flux's (i.e., initial sludge) composition prior to its reaction with any calcium in the crude. As can be seen therein, at point X the flux contains approximately 70 wt. % magnesium chloride and 30 wt. % potassium chloride (referred to hereinafter as M-70 flux). It can also be seen that its liquidus is approximately 520° C., and while such is higher than the starting liquidus of M-130 flux, it is still well below the crude's temperature. It can also be seen that as the reaction proceeds towards point Y, that is, as calcium chloride replaces magnesium chloride, as the liquidus of the sludge actually drops first to a minimum of 460° C. before increasing. Moreover, the maximum theoretical liquidus at point Y is only 680° C. which is below that of the M-130 produced sludge which, as previously mentioned, is approximately 700° C. Moreover, the approximate actual liquidus of the final sludge which is represented by point Z in only 660° C. Accordingly, with M-70 flux of the present invention, it is possible to carry out the reclaim operation at lower temperatures. Less sludge is also produced with M-70 flux as opposed to M-130 flux since less inert potassium chloride is added to the system and no calcium fluoride is added. Flux costs are lower since less flux is used.
A number of flux compositions with various concentrations of magnesium chloride were prepared for testing. Table I sets forth data taken from seven runs in which M-70 flux was added and mixed into a crucible containing magnesium crude which was produced by the process disclosed in U.S. Pat. No. 4,478,637, which hereby is incorporated by reference. In addition to M-70 flux, an M-318 flux having a composition of 50 wt. % KCl, 36 wt. % MgCl2 and 14 wt. % CaF2 and an aluminum fluoride flux were added to the crude during the refining step. M-318 flux is a conventional, generally nonreactive inspissating flux which floats on the surface of the molten crude, thereby acting as a cover flux to prevent the crude from oxidation and/or burning. The aluminum fluoride flux serves to strip oxides from the magnesium droplets which improves magnesium coalescence. This also enhances the oxide's entrapment in the sludge. The presence of aluminum fluoride in the sludge also enhances the subsequent reclaim operation, again by enhancing magnesium coalescence. In run 7 of Table I, it will be noted that a relatively high amount (i.e., 375 pounds) of M-318 flux was added during the refining step. It will be noted, however, that only 960 pounds of M-70 flux were mixed. Thus, in the case, those skilled in the art will appreciate that some of the magnesium chloride in the M-318 flux actually entered the crude to react with the calcium. The fluxes listed under the general heading of reclaim were added to the sludge produced by the refining step to reclaim recoverable magnesium contained therein.
Table II sets forth data taken from a second series of 10 runs in which flux containing 80 wt. % magnesium chloride and 20 wt. % potassium chloride (i.e., M-80 flux) was added and mixed into a crucible containing magnesium crude. Again, varying amounts of M-318 and aluminum fluoride flux were added during the refining step. The sludge produced by the refine step was also reclaimed with the indicated fluxes. In run 8, it will be seen that a relatively high amount of M-318 flux was added for reactive purposes to make up for the relatively small amount (i.e., 900 pounds) of M-80 flux added.
Table III sets forth data taken from a third series of two runs which were conducted with a 100% magnesium chloride flux (i.e., an M-100 flux). Again, it will be noted that high amounts of M-318 flux were added to the crude during the refining operation. The M-318 flux was not added initially, however. It was only added after it was observed that the oxides were not properly settling out into the sludge. The M-100 flux was successful, however, in reducing calcium. Thus, it will be appreciated that while an M-100 flux was initially added, the addition of the extra M-318 actually brought the total composition of the flux used for reaction purposes down close to that of an M-70 flux.
Table IV compares the average results from the three series of tests set forth in Tables I, II and III with the average results obtained using standard M-130 flux. The M-130 results were taken from hundreds of commercial runs. It can be seen in Table IV that the average direct cast results (i.e., which is the percentage of magnesium recovered from the crude by the refining step prior to reclaiming) are substantially better with the M-70, M-80 and M-100 fluxes, particularly the M-70 and M-80, than the averages obtained with standard M-130 flux. For example, the M-70 and M-80 fluxes, respectively, produced average direct cast recoveries of 82.2% and 78.0%, both of which are significantly better than the average direct cast recovery obtained with M-130 flux which is only 72.0%. Similarly, total recovery of magnesium after the reclaiming step is better. The M-70, M-80 and M-100 fluxes achieved average total reclaim recoveries of 91.4%, 89.5% and 91.5%, all of which are significantly better than the average recoveries obtained with the M-130 flux which generally runs between about 86 and 87%. It will also be noted that the M-70, M-80 and M100 tests consumed much less flux than that which is normally consumed when refining with conventional M-130 flux. Accordingly, commercial operation with the high magnesium chloride fluxes of the present invention should significantly reduce flux costs.
While, prior to the tests, it was anticipated that the higher magnesium chloride fluxes of the present invention would translate into flux cost savings and easier reclaims, the higher magnesium recoveries were totally unexpected. Why this occurred is not completely understood. It is speculated, however, that the generation of less sludge by these fluxes may entrap less magnesium in the sludge. This would explain the higher direct cast recoveries which, in turn, enable the higher total reclaim recoveries.
TABLE I__________________________________________________________________________M-70 Flux Tests Direct Refine Reclaim Cast Reclaim Mg Crude M-70 M-318 AlF3 M-130 KCl AlF3 Recovery RecoveryRun (lbs) (lbs) (lbs) (lbs) (lbs) (lbs) (lbs) (%) (%)__________________________________________________________________________1 19230 1320 150 70 375 600 35 80.2 81.62 15570 960 75 70 225 1500 105 86.0 97.43 20050 1260 225 70 150 675 35 85.9 95.34 20500 1320 0 0 750 375 105 77.4 89.65 19640 1200 225 0 300 750 140 87.6 95.96 18850 1140 225 140 225 750 70 82.1 93.17 19990 960 375 70 0 375 35 76.2 86.8avg. 19118 1166 182 60 289 718 75 82.2 91.4__________________________________________________________________________
TABLE II__________________________________________________________________________M-80 Flux Tests Direct Refine Reclaim Cast Reclaim Mg Crude M-70 M-318 AlF3 M-130 KCl Alf3 Recovery RecoveryRun (lbs) (lbs) (lbs) (lbs) (lbs) (lbs) (lbs) (%) (%)__________________________________________________________________________1 21960 1500 75 70 675 300 70 65.8 88.52 18860 1440 225 0 150 675 70 74.2 90.23 18480 1140 150 70 225 375 70 87.3 95.54 18200 1080 150 70 375 600 70 85.2 95.25 21070 1260 75 70 525 1125 105 81.6 91.76 15660 900 300 70 225 1050 70 79.0 88.77 18990 1200 225 0 300 1200 70 77.8 86.18 18950 900 825 70 375 600 105 76.4 85.69 17700 1020 225 70 600 0 0 77.4 86.610 18430 840 225 70 450 750 35 75.4 86.8avg. 18830 1128 248 56 390 668 66 78.0 89.5__________________________________________________________________________
TABLE III__________________________________________________________________________M-100 Flux Tests Direct Refine Reclaim Cast Reclaim Mg Crude M-70 M-318 AlF3 M-130 KCl AlF3 Recovery RecoveryRun (lbs) (lbs) (lbs) (lbs) (lbs) (lbs) (lbs) (%) (%)__________________________________________________________________________1 20360 780 675 0 300 675 140 77.7 91.72 19450 840 675 35 225 900 140 73.9 91.3avg. 19905 810 675 18 262 788 140 75.8 91.5__________________________________________________________________________
TABLE IV__________________________________________________________________________ DirectAverage Total Cast ReclaimCrude Refine Fluxes Reclaim Fluxes Flux Recovery RecoveryFlux (lbs.) M-130 M-70 M-80 M-100 M-318 AlF3 M-130 KCl AlF3 (lbs) (%) (%)__________________________________________________________________________M-130 18,928 2021 -- -- -- 207 125 319 540 48 3260 72.0 86-87M-70 19,118 -- 1166 -- -- 182 60 289 718 75 2490 82.2 91.4M-80 18,830 -- -- 1128 -- 228 56 390 668 66 2536 78.0 89.5M-100 19,905 -- -- -- 810 675 18 262 788 140 2693 75.8 91.5__________________________________________________________________________
While the invention has been described in terms of preferred embodiments, the claims appended hereto are intended to encompass all embodiments which fall within the spirit of the invention.
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|US1524470 *||24 ago. 1921||27 jan. 1925||Firm Chem Fab Griesheim Elektr||Process for recovering light metals from scrap|
|US1754788 *||13 jul. 1923||15 abr. 1930||Dow Chemical Co||Purifying light-metal alloys|
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|US4099965 *||22 set. 1976||11 jul. 1978||Servimetal||Method of using MgCl2 -KCl flux for purification of an aluminum alloy preparation|
|US4384887 *||26 maio 1981||24 maio 1983||The Dow Chemical Co.||Process of making salt-coated magnesium granules|
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|5||*||Lawrence H. Van Vlack, Elements of Materials Science and Engineering (fourth edition), 1980, p. 532, Appendix D.|
|Citação||Data de depósito||Data de publicação||Requerente||Título|
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|EP1878807A1 *||11 jul. 2007||16 jan. 2008||MQP Limited||Method of casting aluminium and aluminium alloy|
|WO1990002209A1 *||28 ago. 1989||8 mar. 1990||The Dow Chemical Company||Process for producing high purity magnesium|
|Classificação nos Estados Unidos||75/604, 75/308|
|25 fev. 1986||AS||Assignment|
Owner name: ALUMINUM COMPANY OF AMERICA, PITTSBURGH, PA. A COR
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNORS:CHRISTINI, ROY A.;FRIZZELL, KENNETH P.;REEL/FRAME:004521/0297
Effective date: 19860216
|9 fev. 1988||CC||Certificate of correction|
|23 abr. 1991||REMI||Maintenance fee reminder mailed|
|22 set. 1991||LAPS||Lapse for failure to pay maintenance fees|
|3 dez. 1991||FP||Expired due to failure to pay maintenance fee|
Effective date: 19910922